Rubber compositions containing hydrocarbon resins



Patented Nov. 6, 1945 RUBB CGMPOSITIONS CONTAINING BOCARBON RESINS Frank J. Soday, Swarthmore, Pa", assignor to The United Gas Improvement Company, a corporation of Pennsylvania No Drawing. Application October 28,1941,

Serial N0. 416,867

8 Claims.

This invention pertains to the use of certain hydrocarbon resins in rubber compositions.

More particularly, this invention relates to the use in rubber compositions of resins derived by the polymerization, by thermal and/or catalytic methods, of certain high boiling monomeric hydrocarbon material recovered as hereinafter referred to from tar formed during the production of combustible gas by processes involving the pyrolytic decomposition of petroleum oil with or without the aid of catalysts.

, It is an object of this invention to provide a rubber composition comprising a mixture with rubber of a certain resin derived from the hydro-- carbon material recovered from. tar, with or without the addition of other ingredients, such as sulfurand/or sulfur compounds, aging inhibitors, oxidation inhibitors, vulcanizing accelerators, carbon, fillers, softening agents, pigments, waxes, other resins, coloring agents, and the like.

Another object of this invention is the provision of rubber compositions comprising one or more natural and/or synthetic rubbers or elastomers and a certain resin derived from the hydrocarbon material recovered from tar, with or without other ingredients.

Still another object of this invention is the provision of rubber blends or compositions possessing qualities superior to those available heretofore, comprising a blend or mixture of one or more synthetic rubbers, elastomers and/or natural rubbers and a certain resin derived from the hydrocarbon material recovered from tar by thermal and/or catalytic means.

Other objects of the invention will be apparent to those skilled in the art upon an inspection of the specification and claims.

I have found that the resin obtained by the thermal and/or catalytic polymerization oi unsaturated monomeric material boiling within the range of from 210 C. to 350 C. and separated in monomeric' form from higher boiling pitch-constituents of the tar iormed during the production of gas by processes involving the pyrolytic decomposition of petroleum oil, with or prise residual tar, dead oil, and light oil. The residual tar comprises the heavy black pitch constituents of the tar together with any oil unseparated therefrom. The dead oil comprises oil separated from the residual tar and boiling higher than say 200-210" C. The light oil comprises oil separated from residual tar and boiling lower thansay 200-210" C.

It has been discovered that very considerable quantities of such resin forming unsaturated monomeric material above referred to, including large quantities of readily heat polymerizable material, may be contained in the tar produced in the vapor phase pyrolysis of crude petroleum oilor a fractionor fractions thereof such as tor example gas oil or residuum oil. This is particularly so in the case of petroleum oil gas tar produced when the pyrolysis is conducted at relatively high temperatures, such for example as in the manufacture oi oil gas or carburetted water gas at average set temperatures above 1300 F. and also particularly so when the oil pyrolvzed is naphthenic, suchas a crude oil classifiable in classes 5 to 7 inclusive, according to the method of classification described in Bureau of Mines Report of Investigations 3279, or a fraction or fractions of such an oil.

The possibility of recovering large quantities of resin forming monomeric unsaturated material boiling in the dead oil range was long unrealized. This was because the usual distillation procedures' for the purpose of petroleum tar dehydrati'on and/or tar fractionation were such as to poly merize the readily heat polymerizable monomers boiling in the dead all range into heavy polymers, which were inextricably mixed with the heavy black residual pitch constituents and lost therein.

,I'n copending application Serial Number 370.608, filed December 18, 1940, by Edwin L. Hall and Howard R. Batchelder, such heat polymerizable' monomeric hydrocarbons boiling in the range of from 210 to 350 C. and separated from the heavy black pitch constituents of the petrowithout the aid of catalysts, is unusually well 5 adapted for blending with rubber generally to give compositions possessing exceptionally good properties. Furthermore, I have found that such resins are unusually satisfactory blending agents tor synthetic rubber compositions, tending to im- .prove, rather than to impair, the propertiesoi such blends.

The hydrocarbon constituents of such petro-- leum tar have usually been considered to comleum tar are described and claimed, together with heat polymers produced therefrom.

In copending application 386.232. filed April 1, 1941, by Waldo C. Ault. there is described and claimed the production of catalytic resins from the heat polymerizable and/or catalytically polymerizable monomeric hydrocarbons boiling within the range of from 210 C. to 350 C. and separated in monomeric form from the heavy black pitch constituents of the petroleum tar.

In the manuiacture of oil gas and carburetted water gas, the tar produced is usually inthe form of an emulsion due to the condensation of hydrocarbon constituents from the gas in the presence of water simultaneously condensed from the gas or otherwise present.

In copending application 342,735, filed June 27, 1940, by Edwin L. Hall and Howard B. Batchelder, which has matured into Patent 2,366,899, granted January 9, 1945, there is described a method of dehydrating such petroleum tar emulsions and of fractionating the hydrocarbon constituents thereof by rapid distillation withthe separation from the heavy pitch constituents of residual tar of such heat polymerizable unsaturated monomeric hydrocarbons boiling in the dead oil range. I

In copending application 353,034, filed August 17, 1940, by Howard R. Batchelder, which has matured into Patent 2,883,362, granted August 21, 1945, there is described the dehydration of such petroleum. tar emulsions and the fractionation of the hydrocarbon constituents thereof with the recovery of monomeric unsaturated heat polymerizable dead oil constituents separate from the heavy black pitch constituents of residual tar, by the solvent extractionof the emulsion with a hydrocarbon solvent such as liquefied propane or butane.

Other processes, for example fractional condensation, might be employed to recover these relatively high boiling unsaturated hydrocarbons in monomeric form and separate from the heavy black pitch constituents of the tar. Also processes for oil pyrolysis which avoid the formation of emulsions, may be employed for the production of the monomeric material. Furthermore,

while it may be preferred to employ petroleum oils or cuts therefrom, which are classifiable in classes to 7 inclusive according to Bureau of Mines Report of Investigations 3279 and particularly in class 7, other oils may be employed.

Whatever process of oil pyrolysis is employed in the production of this monomeric material and whatever process is employed for separating the resultant tar, a very important factor is the exercise of care in the treatment of the tar in order to avoid excessive polymerization of these readily heat polymerizable dead oii constituents and their loss as polymers mixed with the heavy black pitch constituents of the residual tar.

As a result of separation of light oil and dead oil components of the products of such petroleum oil pyrolysis from the residuai tar, without polymerization or with materially reduced polymerization, a substantially pitch-free hydrocarbon material may be separated having a portion boiling within the range of from 210 to 350 C., which may contain from 5% to 30%, and higher, of monomeric unsaturated hydrocarbons readily polymerizable by heat.

' Polymerization may be efiected by heating the total material separated from the residual tar sufficiently to polymerize the readily heat polymerizable monomers boiling within the range of from 210 to 350 C., but insufficiently to appreciably polymerize the heat polymerlzable material contained in lower boiling ranges, such, for instance, as methylstyrenes and styrene. This may be accomplished, for example, by heating with stirring ford hours at 200 C., followed by distillation under vacuum to isolate the resin.

It may-be preferable, however, to first effect a separation by fractional distillation between The heat polymerizable monomeric material.

boiling within the range of 210 to 350 C. is so readily polymerizable by heat, that, in the fractional distillation of the light oil from the dead oil, a portion of the monomeric material is usually unavoidably polymerized and remains as polymer dissolved in the other constituents of. the dead oil afterthe light oil is taken off overhead.

The polymerization of the heat polymerizable unsaturated monomeric material in the separated dead oil may be effected by heating the dead oil with stirring, for example, for four hours at 200 C.

The resin thusproduced, together with any resin produced during the separation of the light oil from the dead oil, may then be isolated by distillation under vacuum.

In the separation of lower boiling hydrocarbon I contain components boiling above 350 C. and

light oil boiling below say 210 C. and dead oil Y boilingabove say 210 C.

there may be present heat polymerizable mono? meric material boiling outside the range of from 210 and 350 C. together with the monomeric material boiling within that range. On polymerization therefore the resin may include polymers derived from monomers boiling outside said range along with polymers derived from monomers boiling within said range.

Exhaustive steam distillations of the resins obtained from the unsaturated monomeric material isolated from tar by the distillation or solvent extraction methods described herein have produced resins having melting points as high as from 185 C. to 200 C. and higher, cube in mer cury, as determined by the method and apparatus described in A. S. T. M. Procedure D61-24, with the following modifications.

1. Mercury is employed in depth of 2 inches instead of water.

2. The cube of resin is rigidly supported by clamping the hook upon which the resin is attached so thatthe top of the cube is 1 inch below the surface of the mercury.

3. A 1 inch immersion thermometer is em- 'ployed and is immersed to that depth.

4. The exact temperature at which the resin becomes visible at the surface of the mercury is recorded as the softening point of the .resin.

5. The melting point of the resin is calculated from the softening point by the following formula.

Melting point C.=softening point C.X 1.25+2 C.

tained-"in greater yields by less exhaustive removal of the associated oils, thus resins ranging from very soft to hard resins having high melting points may be obtained as desired.

It has been usually found that each 6% of associated oils left in the resin ing point about 10 C.

Heat resins having melting points of 120 C.

have been readily produced in yields corresponding to 20 to 30% of the dead oil in'the case of the tar distillate produced in accordance with the process described in copending application Serial No. 312,735 and resins of the same melting point have been obtained in yields as high as of the dead oil in the case of dead oil separated from lowers the melt-' i the range of from 210 to 350 C. to produce on' polymerization by heat a 120 C. melting-point resin in quantity equal to at least 10 percent of thehydrocarbon material boiling within the range from 210 C. to 350 C., and preferably at least 20 percent, or higher, but lower concentrations may be employed.

The color of the resins obtained may vary from yellow to dark brown.

Heat polymer resins produced from dead oil separated from residual tar by the distillation process described in said copending application, Serial No. 342,735, have shown a tendency to be lighter in color than those produced from dead oil obtained from the solvent extraction of tar with propane and butane as described in said cpending application, Serial No. 353,034. Also, heat polymer resins produced from the lower boiling portions of the dead oil have shown a tendency to be lighter in color than heat polymer resins produced from the higher boiling portions, especially such a portion as that boiling in a dead oil out taken from 180 C. to 210 C. undera vacuum equivalent to 20 mm. of mercury, absolute.

The following examples will serve to illustrate the preparation of resins from such unsaturated fractions by thermal polymerization methods.

Example 1 r Approximately 1000 grams of dead oil derived from the rapid distillation of oil gas tar in-acoordance with the process described in said copending application, Serial No. 342,735, and subsequent separation of the distillate, was weighed into a 2-liter 3-necked flask equipped with a thermometer and a short reflux condenser. The oil was then slowly stirred and heated over a Bunsen burner at a liquid temperature of 200 C. (110 C.) for a period of 4 hours. At the conclusion oi. this period, the material was allowed to cool somewhat and was then transferred for distillation to a tared 2-liter flask equipped with a ground glass neck.

The oil was accurately weighed at this point.

The flask was provided with means for measuring vapor temperatures and was connected with condensing apparatus and with means for providing a vacuum, including a pressure control device. Bumping during distillation was avoided by folding several folds of iron wire to such length that one end reached slightly into the neck of the is while the other end rested on the bottom at the flask.

The pressure was reduced to 100 mm. Hg, ab-

tained at that value, and the distillation contin-' ued until a vapor temperature of 195 C. was reached.

During the second stage, the condenser may be cooled by cold water, but care should be taken to avoid the solidification of anthracene, if present. The distillation was conducted rapidly, 5to

- cc. of oil per minute being removed.

When a vapor temperature of 195 C. was reached, the source of heat was removed and air was permitted to enter the apparatus slowly until atmospheric balance was restored.

In the above operation the yield of resin was 29.3%, with an actual melting point of 128 C., which was calculated to be equivalent to a yield of 31.4% at a melting point of 120 C. The color of the resin was light brown.

'A straight run A. S. T. M. distillation of 100 cc. of the original oil gave the following data:

First drop C-- 194 5 cc- C 212 10 cc c 22a 20 cc -i C 234.5 30 cc C- 242.5 cc C 258.5 70 cc C- 283.0 90 cc C 319.0 Decompositionpoint -r C 319.0 Total distillate cc. 8'! Density at 20 C "10107 As pointed out previously. the high boilin monomeric material derived from tar obtained in the pyrolysis of petroleum, by rapid distillation or solvent extraction methods may be polymerized to form resins of the type desired by the application of certain catalysts, either with or without the simultaneous, or otherwise, application of heat.

Catalysts such as mineral acids, for example, sulfuric acid, hydrogen chloride, acids of phosphorus, or acid acting metallic halides or complexes of said halides, preferably organic solvent complexes, as for example, boron trifluoride,

solute, and heat applied by means of a Bunsen burner. The distillation was continued at a pressure of 100 mm. Hg, absolute, until the vapor aluminum chloride, boron trifluoride-diethyl ethercomplex, boron trifiuoride-dimethyl ether complex, boron trifluoride-phenyl ether complex,

boron trifiuoride-phenyl methyl ether complex, boron trifluoride-dioxan complex, boron trifiuoride-toluene complex, corresponding aluminum chloride complexes, and the like, may be emplayed for this purpose.

The metallic halides and their complexes employed are characterized by their ability to hydrolyze in the presence of water to give an acid reaction and, hence, for convenience they may be termed acid acting metallic halides.

Though acid-acting catalysts are preferred. other catalysts may be employed if desired such, for example, as catalysts of the neutral surface type. Examples of such catalysts are activated clays, silica gel, activated carbon, and the like. As an example of a convenient procedure for the production of resins of the type desired with E1; use of sulfuric acid as catalyst, the following ven.

Example 2 ously. The acid is added 1 cc. at a time and the temperature is not permitted to exceed 50 C. The addition of-the acid is continued in this manner of a 10% to 20% aqueous solution of sodium hydroxide. After washing with caustic, an additional water wash may be made- In either case,

the resin solution is dried by-filtration through a I bed of a suitable drying agent, such as lime.

range of from 210 to 350 C. described herein and the resins produced therefrom have shown that these materials are predominately aromatic.

Density determinations have indicated that the density at 25 C. of the resins obtained as above described frequently falls within the approximate range of 1.12 to 1.20, with resins produced from dead oil from the solvent extraction of tar tending to be somewhat higher than those produced from dead oil from rapid tar distillation. The densities of the acid polymers tend to be somewhat lower than those of the heat polymers derived from the same unsaturated dead oil. Resins of If desired, the diluent may be added before polymerization instead of after polymerization.

After neutralization and drying, the resin may be isolated from the unpolymerized oil by any desired method, or the resin may be concentrated therein by vacuum distillation, which may be assisted by steam. The melting point of the resin and the yield obtained will depend, among other things, upon the extent to which the resin has been removed from the unpolymerized oil.

Example 3 A 532.6 gram portion of this unsaturated dead oil was treated with 8 cc. of 66 B. H2804 according to the procedure described in Example 2. Toluene was added after polymerization. Approximately 42% of the'dead oil was converted to resin having a melting point of 97 C. and a brown color. The end temperature of the distillation for the removal of oil from the resin was 192 C. and the end pressure was equivalent to 18 mm. of mercury, absolute. A total of 145.9 grams of oil was recovered. The calculated yield of resin having a melting point of 120 C. was 36.2%.

As pointed out previously, the unsaturated dead oil employed for the preparation of resins of the type desired may be polymerized by (a) thermal means, (b) catalytic means, or (c) a combination of thermal and catalytic means. In the latter case, the processes may be carried out consecutively without the intermediate removal of resin, or the resin may be removed between successive treatments.

The unsaturate dead oil used in the following example was obtained from petroleum tar emul-- sion by the process of copending application Serial I Number 342,735. After separation from light oil, it was treated to remove heat polymerizable unsaturates by heating at 200 C. for 4 hours, fol-' lowed by removal'of the heat polymer resin formed. It wasthen subjected to catalytic polymerization by the following method.

Example 4 v oilwas treated with 6 cc. of 66 Be. H2804 accordthis type having other densities may be employed,

however.

The molecular weights of the resins produced as previously described necessarily vary with the melting point, which also varies with the presence of varying quantities of associated oil among other factors. Determinations by the Benzene freezing point depression method have shown that such resins usually have molecular weights ranging from 308 to 758 over a range of melting points from 80.5" C.to 195 C. as determined by the cube in mercury method.

The fracture of the high melting point resins described herein may range. from conchoidal to hackly. Ingeneral, the polymers are quite brittle.

The resins described herein, except those hardened by exhaustive steam distillation to a very high melting point, will usually react positively to the anthraquinone reaction, indicating the presence of anthracene, unless produced from lower boiling portions of the dead oil, which do not contain anthracene, or unless the anthracene has been otherwise removed.

ing to the method described in Example 2. Naph-- the. was added after polymerization. Approximately 19% of the dead oil was converted to,

resin having a melting point of 882 C. and a light yellow brown'color. The end temperature of the distillation for the removal of oil from the resin was 185 C., and the and pressure was equivalent to 20 mm. of mercury, absolute. A'total of 407.9 grams of oil was recovered. The calculated yield of resin having a melting point of 120 C.

was approximately 15%. I

Examination of the monomeric unsaturated material and associated oil boiling within the but a slight diazo reaction,

' scribed in The resins described herein usually will give indicating the substantial absence of phenols;

The resins produced as above described usually will give negative Lieberman Storch reactions, indicating the absence of rosin acids.

Upon thermal decomposition of the resins of the type produced as above described herein, appreciable yields of material boiling within the range from 210 C. to 350 C. will be produced.

The heat polymer resins of the type produced as abovedescribed usually are substantially completely soluble in carbon disulflde and benzol.

The quantity of resin insoluble in a mixture containing 50% petroleum ether and 50% pentane varies with the melting point of the resin, and may be of the order of 52% in the case of a thermal resin having a melting point of 95 C. and of the order of iii the case of a thermal resin having a melting point of approximately 183 C.

The quantity of resin of the type produced as above described insoluble in a mixture of 50% petroleum ether and 50% pentane, but soluble in CCh, may be of the order of 50% for a thermal resin having a melting point of C. and of the order of 74% in the case of a thermal resin having a'melting point of 183 C.

The quantity of thermal resin insoluble in both the petroleum ether pentane solution and C014 usually is very low, ranging from a fraction of a percent to the neighborhoodof 6 or 7%.

In generaLcatalytic polymers are much-more soluble than heat polymers from the same ungatlgrated dead oil in all solvents except the alco- The polymers from unsaturated dead oils obtained from the rapid distillation process decopending application, Serial No. 342,735, tend to be more soluble in those solvents a tried than similarly producedpolymers from unsaturated dead oils obtained by the solvent extraction process described in copending application, Serial .No. 353,034.

The above described characteristics of color, density, fracture, melting point, molecular weight, diazo reaction, Lieberman Storch reaction, anthraquinone reaction, thermal decomposition, and solubility are given for the purpose of illustration. It is not intended to imply necessarily that the resin produced as described above and employed herein may not depart somewhat from this illustrative description in one particular or more.

Furthermore, the addition of other materials to the heat polymerizable monomeric unsaturated materials prior to polymerization or to the resins afterpolymerizatio'n may of course modify the properties of the resins produced. Examples of such materials are other synthetic or natural resins, plasticizers, softeners, fillers, coloring materials, etc.

The resin employed may comprise mixed polymers of monomeric material boiling throughout the range of from 210 C. to 350 C. together if desired with polymers of monomers boiling outside of this range or resins may be employed which are produced from monomers boiling within a selected range or ranges within the range of from 210 C. to 350 C., for instance from separated material boiling above say 250 C. or say above 280 C.

. In separating such material, the dead oil con taining the monomers maybe fractionated by distillation'under vacuum assisted by steam to avoid undue polymerization during the separation, or other methods of separation may be employed- As previously pointed out, the herein described resins, namely; those obtained by the thermal and/or catalytic-polymerization of the unsaturated monomeric material recovered from the tar formed during the production of gas by processes involving the pyrolytic decomposition or conversion of hydrocarbon oil, with or without the aid of catalysts, are unusually well adapted for blending with rubber, and particularly with synthetic rubbers or elastorners, to give compositions possessing exceptionally good properties. As blending agents for synthetic rubbers or elastomers, they enhance, rather than detract from, the wearing and other desirable properties of such materials in many cases.

Examples of the rubber or rubber-like materials with which these resins may be compounded are the various grades and types of natural rubber and rubber-like materials, and synthetic rubbars or elastomers, such as, for example, those obtained by the polymerization of one or more dioleflnes, or substituents thereof, such as butadiene, isoprene, piperylene, 2-chlorobutadiene,-

and the like, either alone, or in admixture, or in combination with one or more unsaturated and/ or reactive compounds or materials such as olefines, unsaturated nltriles, acids, esters, ethers, ketones,

' asbestine, factice, and glue, softeners, such as,-for.

aldehydes, and/hr substituents thereof, such as.

Chloroprene, Neoprene, Ameripol, Hycar, Butyl rubber, and the like.

The quantity of resin or the type described herein which may be incorporated in natural or synthetic, rubbers, or elastomers, may be varied over very wide limits, depending upon the properties desired. Thus, for example, quantities varying from a few percent, or less, to an amount equal to, or greater than, the quantity of rubber, or rubber mixture, employed in thecomposition, may be used.

In addition to resins of the type described herein, other ingredients which may be incorporated in natural rubber and/or synthetic rubber compositions include vulcanizing agents and/ or accelerators, such as, for example, sulfur or sulfurcontainingcoinpounds such as tetramethylthiuram disulfide, mercaptoarylenethiazoles, and dithio carbamates, metallic oxides, such as, for example, magnesium oxide, zinc oxide, and lead oxides, antioxidants, such as, for example,

phenyl-alpha-naphthylamine (Neozone A), and

phenyl-beta-naphthylamine (Neozone D), rein forcing pigments, such as, for example, carbon blacks, clay, and blanc flxe, fillers and/or diluents, such as, for example, lithopone, barytes,

example, paraffin wax, oils, fatty acids, andother synthetic or natural resins and/or deodorants, 'such as terpene compounds.

Reclaimed rubber is also includedamong the materials which may be blended with the hydrocarbon resins herein described together with nat-" ural and /or synthetic rubber and with or without other ingredients.

The resin, and other ingredients, may be mixed Example 5 Component: Parts by weight Natural rubber 10d Resin 2d Magnesium ox'ide 5 Sulfur 2.5 Mercapt'obenzothiazole 01a Example 6 Component: Parts by weight Pale crepe rubber Zinc oxide 50 Sulfur 2.5 Resin 5 Stearic acid 0.3 Mercapto benzothiazole 0.6

Example 7 A natural rubber tire tread mix may be comp unded as follows:

Component: Parts by weight Smoked sheet rubber 100 Carbon black 40 Zinc mride 6 Stearic acid l Resin 5 Sulfur 3 Mercapto benzothiazole----- Emmple 8 A synthetic rubber tire tread mix may be compounded as follows:

Component: Parts by weight Neoprene 100 Resi 4 5 Light calcined magnesia '10 Carbon black v 05 Pine tar Phenyl-s-naphthylamine-....-..' 2 Suliur 1 Zinc oxide 5 Emmple 9 Component: Parts by weight Butadiene-styrene rubber 100 Resin 5 Carbon black 4..---. 35 Suliur Mercapto benzothiazole 0.8 Zinc oxide 10' Phenyl-a-naphthylamine 2 Example 10 Component:

Butadiene-acrylic nitrile rubber..."- 100 Resin 10 Carbon black 25 Sulfur I s Mercaptobenzothiazole...-....-..-.-s..- 0.7! Light calcined magnesia---='-..-- 10 Phenyl-a-naphthylamine '2 Emmpleii Component:

Butadiene-isobutylene rubber 100 Resin 10 "Carbon black.

Sulmr v Mercapto benzothiazole Phenyl-s-naphthylamine 1 Oxide ---------'m.- a

The foregoing compositions may be sheeted out, shaped and vulcanized, such as by the. application of a temperature of say 140 C. in a press for a period of say 45 minutes. Other procedures may, 01' course, be used ii desired.

While various procedures and formulas have been particularly described these are of course subject to considerable variation. Therefore, it will be understood that the foregoing specific examples are given by way 0! illustration, and that changes, omissions, additions, substitutions v and/or modifications might be made within the scope of the claims without departing irom the spirit or theinvention, which is intended to be limited only as required by the prior art.

I claim:

application to said oil of heat alone but which are polymerizable to catalytic resin polymer by treating said oil with a resin-producing catalyst,

. other hydrocarbons boiling between 210 C. and 5 350 C. which are polymerizable to catalytic resin polymer by treating said 011 with a resin-producing catalyst but which last-mentioned hydrocarbons are also polymerizable to heat resin polymer by the application to said all of heat alone, said 3 l0 last-mentioned hydrocarbons being present in said hydrocarbon oil in amount greater than approximately 5% of the total hydrocarbon oil boiling between 210 C. and 350 C.

2. A composition comprising rubber selected 35 from the group consisting of natural rubber and rubber-like polymers of butadiene, isoprene, piperylene and 2-chlorobutadiene, and from 5% to based on said rubber of hydrocarbon resin polymer selected from the group consisting of 8 20. heat resin polymer and catalytic resin polymer of polymerizable hydrocarbons contained in a hydrocarbon oil which has been physicallyseparated from tar produced in the vapor phase pyrolysis of petroleum oil and which is free from and of Parts by weight as greater volatility than the pitch of said tar, said hydrocarbon oil when separated and when subjected to polymerization containing in addition to hydrocarbons boiling between 210 C. and 350 C. which are not polymerizable by the application to said oil of heat alone but which are polymerizable to catalytic resin polymer by treating said oil with a resin-producing catalyst, other hydrocarbons boiling between 210 C. and 350 C. which are polymerizable to cata- Parts by weight 85 lytic resin polymer brtreating said oil with a resin-producing catalyst but which last-mentioned hydrocarbons are also-polymerizable to heat resin polymer by the application to said oil of heat alone, said last-mentioned hydrocarbons being present in said hydrocarbon oil in amount greater than approximately 5% 01! the total hydrocarbon oil boiling between 210 C. and 350 C. g

. 3. A composition comprising rubber-like copolymer of butadiene and styrene, and from 5% to 20% based on said-copolymer of hydrocarbon resin polymer selected from the group consisting of heat resin polymer and catalytic resin polymer of polymerizable hydrocarbons contained in a hydrocarbon oil which has been physically sepasubjected to polymerization containing in addition to hydrocarbons bolllngbetween 210 C. and

350 C, which are not polymerizable by the application tosaid oil of heat alone but which are polymerizable to catalytic resin polymer by treat- .1. A composition comprising rubber selected log said oil with a res -p oducin catalys ot r from the group consisting of natural rubber and rubber-like polymers of butadiene, isoprene, piperylene and 2-chlorobutadiene,',and from 5% to 100% based on said rubber of hydrocarbon resin polymer selected from the group'consisting pyrolysisof petroleum oil and which is free from and 01' greater volatility than the pitch oi said tar, saidhydrocarbon oil when separated and ,when subjected to polymerization containing in addition to hydrocarbons boiling between 210 C.

hydrocarbons boiling between 210 C. and 350 C. 1 which are polymerizable to catalytic resin polymer by treating said 011 with a resin-producing catalyst but .which last-mentioned hydrocarbons 05 are also polymerizable to heat resin polymer by the application to said 011 of heat alone. said lastmentioned hydrocarbons being present in said hydrocarbon oil in amount greater than approximately 5% of the total hydrocarbon oil boiling between 210 C. and 350 C.

4. A composition comprising rubber-like copolymer or butadiene and acrylic nitrile, and from 5% to 20% based on said copolymer of hydrocarbon resin polymer selected from the' and 350 c. which are not p lymerizable y the s ms of heat resin polymer and c tsaseaecc r a 7 lytic resin polymer of polymerizable hydrocara w contained in a hydrocarbon oil which has been physically separated from tar produced in the vapor phase pyrolysis of petroleum oil and which is free from and of greatervolatility than the pitch of said tar, said hydrocarbon oil when separated and when subjected to polymerization containing in addition to hydrocarbons boiling between 210 C. and 350 C. which are not poly-- merizable by the application to said oil of heat alone but which are polymerizable to catalytic resin polymer by treating said oil with a resinproducing catalyst, other hydrocarbons boiling between 210 C. and 350 C. which are polymerizable to catalytic resin polymer by treating said oil with a resin-producing catalyst but which lastmentioned hydrocarbons are also polymerizable to heat resin .polymer by the application to said oil or heat alone, said last-mentioned hydrocarbons being present in said hydrocarbon oil in amount greater than approximately of the total hydrocarbon oil boiling between 210 C. and

5..A composition comprising natural rubber, and i'rom 5% to 20% based on said rubber oi hydrocarbon resin polymer selected from the group consisting of heat resin polymer and catalytic resin polymer of polymerizable hydrocarbons contained in a hydrocarbon oil which has been physically separated from tar produced in the vapor phase pyrolysis of petroleum oil and which is free from and of greater volatility than the pitch of said tar, said hydrocarbon'fiil when separated and when subjected to polymerization containing in addition to hydrocarbons boiling between 210 C. and 350 C. which are not polymerizcble by the application to said oil oi heat alone but which are polymerizable to catalytic resin polymer by treating said oil with a resinproducing cataLvst, other hydrocarbons boiling between 210 C. and 350 C. which are polymerizable to catalytic resin polymer by treating said oil with a resin-producing catalyst'but which l'astmentioned hydrocarbons are also polymerizable to heat resin polymer by the application to said oil of heat alone, said last-mentioned hydrocars bons being present in said hydrocarbon oil in amount greater than approximately 5%oi' the gostal hydrocarbon oil boiling between 210 C. and

cation to said oil of heat alone but which are porizable to catalytic resin polymer by treatins said oil with sulfuric acid, other boiling between 210' C. and 350 C. which are polymerizable to catalytic resin polymer by treating said 011 with sulfuric acid but which lastmentioned hydrocarbons are also polymerizable to heat resin polymer by the application to said 011 of heat alone, said last-mentioned hydrocarbons being present in said hydrocarbon oil in amount greater than approximately 5% o! the total hydrocarbon oil boiling between 210 C. and 350 C.

'7. A composition comprising rubber-like copolymer of butadiene and acrylic nitrile, and

from 5% to 20% based on said copolymer of heat resin polymer produced by the application of heat to a hydrocarbon oil which has been physically separated from tar produced in the vapor phase pyrolysis of petroleum oil and which is i'ree from and of greater volatility than the pitch of said tar, said hydrocarbon 011 containing in addition to hydrocarbons boiling between 210 C. and 350- C. which are not polymerizable by the application to said oil of heat alone but which are polymerizable to catalytic resin polymer by treating said oil with a resin-producing catalyst. other hydrocarbons boiling between 210' O. and 350 C. which are. polymerizable to catalytic resin polymer by treating said oil with a resin-producing catalyst but which last-mentioned hydrocarbonsare also polynierizable to heat resin polymer by the application to said oil 01' heat alone, said lastmentioned hydrocarbons being present in said,

hydrocarbon oil in amount greater than approximately 5% of the total hydrocarbon oil boiling between 210 (2. and 350 C.

8. A composition comprising :natural rubber, and trom5% to 20% basedonsaid rubber of heat resin polymer produced by the application of heat to a hydrocarbon oil which has been physically separated from tar produced in the vapor phase pyrolysis of petroleum oil and which isiree 6. A composition comprising rubber-likev copolymer of'butadiene and styrene, and from 5% to 20% based on said copolymer of hyarbon resin polymer produced by treating with sulfuric acid a hydrocarbon oil which has been physically separated from-tar produced in the vapor phase pyrolysis of petroleum oil and which is free th n and of greater volatility than the pitch of said tar, said hydrocarbon oil cont in addition to hydrocarbons boiling' between 210 C. and 350 C. which are not pokvmerlnable by the appliiromand oi greater volatility than the pitch of said tar, said hydrocarbon oil containing in addition to hydrocarbons boiling between 210C. and 350 C. which are not polymerizable by the application to said oil of heat. alone but which are polymerizable to catalytic resin polymer by treating said oil with a resin-producing catalyst, other hydrocarbons boiling between 210. C. and 350 C. which are polymerizable to catalytic resin polymer by treating said oil with a resin-producing. catalyst but which last-mentioned hydrocarbons are also pclymerisable wheat resin P lymer by the application to said oil or heat alone. said lastmentioned hydrocarbons being present in said hydrocarbon oil in amount greater than approximately 5% oi the total hydrocarbon oil boiling between 210 C. and 850 C.

, FRANK J. SODAY. 

